JP2015506821A5

JP2015506821A5 -

Info

Publication number: JP2015506821A5
Application number: JP2014546274A
Authority: JP
Filing date: 2012-04-13
Publication date: 2015-04-16
Anticipated expiration: 2032-04-13

Description

本発明に記載する触媒組成におけるほかのモレキュラーシーブは、Y型ゼオライト、Lゼオライト、ZSM-5ゼオライト、βゼオライト、リン酸アルミニウムゼオライト、Ωゼオライトから選ばれる1種又は1種以上ものもであり、好ましいのはY型ゼオライト、ZSM-5ゼオライト、βゼオライト、或は上記のゼオライトの通常の物理又は化学変性されたものであり、HY、USY、REY、REHY、REUSY、H-ZSM-5、Hβを含む。 Other molecular sieves in the catalyst composition described in the present invention are Y type zeolite, L zeolite, ZSM-5 zeolite, β zeolite, aluminum phosphate zeolite, and one or more types selected from Ω zeolite, Preferred is Y-type zeolite, ZSM-5 zeolite, β- zeolite, or the usual physical or chemical modification of the above-mentioned zeolite, HY, USY, REY, REHY, REUSY, H-ZSM-5, H Contains β .

実施例に用いられる原料の仕様について
１．NaYモレキュラーシーブ：NaY-1(ケイバン比4.8、結晶化度92%)、NaY-2(ケイバン比4.1、結晶化度83%)、蘭州石化社触媒工場製。
２．超安定1交換1焼成モレキュラーシーブサンプル：結晶化度60%、酸化ナトリウム4.3m%、蘭州石化社触媒工場製。
３．希土類溶液：塩化希土類(酸化希土類277.5g/l)、硝酸希土類(酸化希土類252g/l)、いずれも工業製品であり、蘭州石化社触媒工場から得られるもの。
４．セスバニア粉、ホウ酸、尿素、エタノール、ポリアクリルアミド、シュウ酸、アジピン酸、酢酸、ギ酸、塩酸、硝酸、クエン酸、サリチル酸、酒石酸、デンプンはいずれも化学用ものであり；塩化アンモニウム、硝酸アンモニウム、硫酸アンモニウム、シュウ酸アンモニウムはいずれも工業製品である。
５．擬ベーマイト(熱灼減量36.2%)、カオリン(熱灼減量16.4%)、ハロイサイト(熱灼減量21.4%)、モンモリロナイト(熱灼減量15.8%)、パーライト(熱灼減量17.6%)は、固体であり；アルミニウムゾルは酸化アルミニウムを23.0重量％含み；シリコンゾルはシリカを24.5重量％含み、いずれも工業合格品である。
６．REY、REHY、USY、REUSYモレキュラーシーブは、いずれも合格工業品であり、蘭州石化社触媒工場製；βゼオライトは、工業合格品、撫順石化社製；H-ZSM-5は、工業合格品、上海復旦大学製。 About specifications of raw materials used in Examples 1. NaY molecular sieve: NaY-1 (Kayban ratio 4.8, crystallinity 92%), NaY-2 (Kayban ratio 4.1, crystallinity 83%), manufactured by Lanzhou Petrochemical Co., Ltd. Catalyst Factory.
2. Ultra-stable 1 exchange 1 calcined molecular sieve sample: 60% crystallinity, 4.3m% sodium oxide, manufactured by Lanzhou Petrochemical Company.
3. Rare earth solution: rare earth chloride (rare earth oxide 277.5g / l), rare earth nitrate (rare earth oxide) 252g / l), both industrial products, obtained from Lanzhou Petrochemical's catalyst factory.
4). Sesbania powder, boric acid, urea, ethanol, polyacrylamide, oxalic acid, adipic acid, acetic acid, formic acid, hydrochloric acid, nitric acid, citric acid, salicylic acid, tartaric acid, starch are all for chemical use; ammonium chloride, ammonium nitrate, ammonium sulfate Ammonium oxalate is an industrial product.
5. Pseudo boehmite (heat loss 36.2%), kaolin (heat loss 16.4%), halloysite (heat loss 21.4%), montmorillonite (heat loss 15.8%), perlite (heat loss 17.6%) are solid Aluminum sol contains 23.0% by weight aluminum oxide; silicon sol contains 24.5% by weight silica, both of which are industrially acceptable.
6). REY, REHY, USY, and REUSY molecular sieve are all acceptable industrial products, manufactured by Lanzhou Petrochemical Co., Ltd .; β- zeolites are industrially acceptable products, manufactured by Fushunishi Chemical; H-ZSM-5 is industrially acceptable products, Made by Shanghai Fudan University.

水浴加熱付の反応槽に、水4.620リットル、カオリン1024g、擬ベーマイト971g及び塩酸90.8mlを添加して均一に混合し、1時間攪拌した後、変性モレキュラーシーブB-1 338g、βゼオライト129g、REHY 806gを順に添加し、均一に混合された後アルミニウムゾル1304gを徐々に加えゲル化し、噴霧成形を経て、得られた微小球を400℃で1.0時間焼成させた。焼成された微小球2kgを取り、脱イオン水20kgを入れて35℃で40分間洗浄し、濾過乾燥して本発明に調製される分解触媒が得られ、Bと表記する。 In a reaction bath with water bath heating, 4.620 liters of water, 1024 g of kaolin, 971 g of pseudoboehmite and 90.8 ml of hydrochloric acid were added and mixed uniformly. After stirring for 1 hour, 338 g of modified molecular sieve B-1 129 g of β zeolite, REHY 806 g was added in order, and after mixing uniformly, 1304 g of aluminum sol was gradually added to gel. After spray molding, the resulting microspheres were fired at 400 ° C. for 1.0 hour. Take 2 kg of calcined microspheres, add 20 kg of deionized water, wash at 35 ° C. for 40 minutes, filter and dry to obtain the cracking catalyst prepared in the present invention, which is denoted as B.

Claims

In the composition of the catalyst, 2 to 50% by weight of ultra-stable rare earth Y-type molecular sieve, 0.5 to 30% by weight of one or more other molecular sieves, 0.5 to 70% by weight of clay, 1.0% of high-temperature inorganic oxide A heavy oil catalytic cracking catalyst comprising ~ 65 wt% and rare earth oxide 0.01 to 12.5 wt%,
The ultra-stable rare earth Y-type molecular sieve is obtained by a preparation process including rare earth exchange and dispersion pre-exchange, containing 0.5 to 25% by weight of rare earth oxide, 1.2% by weight or less of sodium oxide, and crystallinity of 40 to 40%. 75%, lattice constant is 2.449nm ~ 2.472nm,
Rare earth exchange and dispersion pre-exchange are not limited sequentially but are performed continuously, and there is no firing process between them,
In the dispersion pre-exchange, the concentration of the molecular sieve slurry is adjusted to 80 to 400 g / L as the solid content, and the dispersion pre-exchange is performed by adding 0.2 to 7 wt% of the dispersant, and the exchange temperature is 0 to 100 ° C, replacement time is 0.1-1.5 hours,
The above dispersant in the dispersion pre-exchange is selected from sesbania powder, boric acid, urea, ethanol, polyacrylamide, acetic acid, oxalic acid, adipic acid, formic acid, hydrochloric acid, nitric acid, citric acid, salicylic acid, tartaric acid, benzoic acid, starch One or more types
A heavy oil catalytic cracking catalyst characterized in that no ammonium salt is used in rare earth exchange or dispersion pre-exchange.

The other molecular sieve is one or more selected from Y zeolite, L zeolite, ZSM-5 zeolite, β zeolite, aluminum phosphate zeolite, Ω zeolite, or modified zeolite described above. 2. The catalyst according to claim 1.

2. The catalyst according to claim 1, wherein the other molecular sieve is one or more of HY, USY, REY, REHY, REUSY, H-ZSM-5, and β zeolite.

2. The catalyst according to claim 1, wherein the clay is one or more selected from kaolin, halloysite, montmorillonite, sepiolite, and pearlite.

_2. The catalyst according to claim 1, wherein the high temperature resistant inorganic oxide is one or more selected from Al ₂ O ₃ , SiO ₂ , SiO ₂ —Al ₂ O ₃ , and AlPO ₄ .

During the catalyst production process,
(1) The molecular sieve slurry is not limited to the raw material, and the molecular sieve slurry is subjected to rare earth exchange and dispersion pre-exchange, and the molecular sieve slurry is further filtered, washed with water, and fired for the first time. Ultra-stable rare earth Y molecular sieves can be obtained by obtaining sodium Y molecular sieves, and reducing sodium by ammonium salt exchange in the “one-exchange-one-fired” rare earth sodium Y molecular sieves and firing the second time to obtain ultra-stable rare-earth Y-type molecular sieves. The sheave preparation process;
(2) Preparation of a heavy oil catalyst that can be obtained by mixing and homogenizing the above ultrastable rare earth Y-type molecular sieve with clay and high-temperature resistant inorganic oxide precursor, followed by spray molding, firing and washing with water. Process,
2. The method for producing a catalyst according to claim 1, comprising:

Upon rare earth exchange, the RE ₂ O ₃ / Y zeolite mass ratio is 0.005-0.25, exchange temperature is 0-100 ° C., exchange pH value is 2.5-6.0, exchange time is 0.1-2 hours 7. The method for producing a catalyst according to claim 6, wherein

6. In the dispersion pre-exchange, the amount of dispersant added is 0.2 wt% to 7 wt%, the exchange temperature is 0 to 100 ° C., and the exchange time is 0.1 to 1.5 hours. The manufacturing method of the catalyst as described in 1 ..

Upon rare earth exchange, its RE ₂ O ₃ / Y zeolite mass ratio is 0.01 ~ 0.20, exchange temperature is 60 ~ 95 ° C, exchange pH value is 3.5 ~ 5.5, exchange time is 0.3 ~ 1.5 hours In the dispersion pre-exchange, the amount of the dispersant added is 0.2 wt% to 5 wt%, the exchange temperature is 60 to 95 ° C., and the exchange time is 0.1 to 1.5 hours. 7. A method for producing the catalyst according to claim 6.

7. The method for producing a catalyst according to claim 6, wherein the molecular sieve slurry does not have to be washed and filtered between the rare earth exchange and the dispersion pre-exchange, and may be washed and filtered.

7. The method for producing a catalyst according to claim 6, wherein pot-type exchange, belt-type exchange and / or cake exchange are employed in the rare earth exchange or dispersion pre-exchange exchange process.

The rare earth compound solution is divided into a plurality of parts when performing rare earth exchange, pot type exchange, belt type exchange and / or cake exchange are performed, that is, a plurality of exchanges are performed. A method for producing a catalyst.

In the dispersion pre-exchange process, the dispersant is divided into a plurality of parts, pot-type exchange, belt-type exchange and / or cake exchange is performed, that is, a plurality of exchanges are performed. Production method.

7. The method for producing a catalyst according to claim 6, wherein when the rare earth exchange and the dispersion preliminary exchange are a plurality of exchanges, the two kinds of exchanges are alternately performed.

7. The method for producing a catalyst according to claim 6, wherein the calcining conditions for the first calcination of the molecular sieve are calcination at 350 ° C. to 700 ° C. and 0 to 100% steam for 0.3 to 3.5 hours.

7. The method for producing a catalyst according to claim 6, wherein the precursor of the high temperature resistant inorganic oxide is selected from silica alumina gel, silica sol, alumina sol, silica alumina composite sol, and pseudoboehmite.

13. The method for producing a catalyst according to claim 12, wherein the rare earth compound is a rare earth chloride, a rare earth nitrate, or a rare earth sulfate.

18. The method for producing a catalyst according to claim 17, wherein the rare earth described in the present invention is lanthanum enriched rare earth, cerium enriched rare earth, pure lanthanum, or pure cerium.

7. The method for producing a catalyst according to claim 6, wherein the calcination conditions in step (2) are that the sprayed microspheres are calcined at 200 ° C. to 700 ° C. and the time is 0.05 to 4 hours.

7. The method for producing a catalyst according to claim 6, wherein the calcination conditions in the step (2) are that the sprayed microspheres are calcined at 300 ° C. to 650 ° C. and the time is 0.1 to 3.5 hours.

7. The method for producing a catalyst according to claim 6, wherein water washing conditions in step (2) are: water / catalyst weight of 0.5 to 35, water washing temperature of 20 ° C. to 100 ° C., and time of 0.1 to 0.3 hours. .